Method and apparatus for high pressure sterilization

ABSTRACT

A process for sterilization of a liquid in a continuous system comprising a series of steps. First the liquid is continuously pumped into a pressurized system. Second, the pressure on the liquid is increased in a first pressurization stage. Next, the liquid is increased in pressure in a second pressurization stage. Fourth, the liquid is held at an elevated pressure for a predetermined period of time to kill off microorganisms within the liquid. The liquid is then rapidly depressurized to fracture microorganisms within the liquid. The apparatus for producing this process includes a continuous liquid treatment system with a pump, a first stage intensifier, a surge drum, a second stage intensifier, a pressure receiver and a pressure reducer. A particulate treatment system may also be included which comprises a pressure receiver, an intensifier, and a recoverer for blending a particulate component with the liquid component.

FIELD OF THE INVENTION

[0001] The present invention relates to a continuous process for thesterilization or deactivation of microorganisms in liquids, such asliquid foods and beverages.

BACKGROUND OF THE INVENTION

[0002] Many liquids, such as commercial processed foods, including, butnot limited to, juices, beverages, soups and stews, containmicroorganisms that continue to multiply after processing therebyreducing the safe shelf life of the foods. It is has been known thatexposure of microorganisms to very high pressures (e.g. up to 100 kpsi)will reduce the population of various species of microorganisms duringbatch processing. Furthermore, the high pressure treatment of liquidfoods, while deactivating microorganisms, has essentially no negativeeffect on the taste and appearance of the liquid.

[0003] The prior art generally discloses complicated batch processes andapparatus for the deactivation of microorganisms in a liquid.Unfortunately, batch processes can be expensive and inefficient.

SUMMARY OF THE INVENTION

[0004] In accordance with the teachings of the present invention, aprocess and an apparatus for the sterilization of a liquid are providedwhich substantially eliminate or reduce disadvantages and problemsassociated with prior art devices and techniques. In particular, theprocess for sterilizing a liquid (which may be a liquid component aloneor a liquid component and a particulate component) includes increasingthe pressure on the liquid, and rapidly reducing the pressure on theliquid component while maintaining the liquid within an acceptabletemperature range.

[0005] To produce this process, there is provided an apparatus thatincludes a pump for introducing a liquid into a pressurized system. Thepump is coupled with a first stage intensifier for increasing thepressure of the liquid. A second stage intensifier is coupled to thefirst stage intensifier to further increase the pressure on the liquid.Although the two-stage increase is preferred, a single stage could alsobe used. A pressure receiver is connected to the second stageintensifier, the pressure receiver for maintaining the pressure on theliquid for a predetermined period of time. Finally, a pressure reduceris attached to the pressure receiver wherein the pressure reducerreceives the liquid and reduces the pressure on the liquid toatmospheric pressure. In addition, a particulate component treatmentapparatus can be provided, which includes a receiver, an intensifier,and a mixer, for mixing the particulate component with the liquidcomponent, if particulate components are provided. The particulatecomponent treatment apparatus can also be used on the liquid components,and thus a mixer may not be needed in such cases.

[0006] One important technical advantage of the present invention is thefact that it provides a continuous system for sterilizing a liquid,thereby reducing the strain on the apparatus from the repeated cyclingof pressurization in the system, and increasing system efficiency.Another important technical advantage of the present invention is thatit can be repaired without interrupting the continuous process forsterilization of liquid within the system.

BRIEF DESCRIPTION OF THE DRAWINGS

[0007]FIG. 1 is a block flow diagram of the total deactivation process.

[0008]FIG. 2 is a block flow diagram of the supercritical pressureliquid treatment process

[0009]FIG. 3 is a schematic diagram of the liquid supercritical pressuretreatment apparatus.

[0010]FIG. 4 is a schematic diagram of the supplemental maintenancecontrol system.

[0011]FIG. 5 is a schematic cross sectional view of stainless steellined high pressure tubing.

[0012]FIG. 6 illustrates the intensifier system pressure relief system.

[0013]FIG. 7 is a schematic view of the pressure let down station.

[0014]FIG. 8 is a is a cross sectional drawing of the design for acontrollable high pressure high velocity pressure/flow control valve.

[0015]FIG. 9 is a cross-sectional view of orifice pressure/flow controlsystem.

[0016]FIG. 10 illustrates the thermodynamics of the pressure let downstation.

[0017]FIG. 11 is a block flow diagram showing the particulate treatmentprocess.

[0018]FIG. 12 is a schematic diagram of the single receiverconfiguration of the particulate treatment apparatus.

[0019]FIG. 13 is a schematic diagram of the multiple receiverconfiguration of the particulate supercritical pressure treatmentapparatus.

[0020]FIG. 14 is a cross sectional diagram illustrating the pulptreatment batch receiver.

[0021]FIG. 15 is a cross sectional drawing of a Graylock coupling usedto connect the lined high pressure process tubing.

[0022]FIG. 16 is a cross sectional drawing of a first pressurization endplug for the treatment apparatus.

[0023]FIG. 17 is a cross sectional drawing of a second pressurizationend plug for the treatment apparatus.

DETAILED DESCRIPTION OF THE INVENTION

[0024] Throughout the following discussion, specific pressures,temperatures, times, and other parameters, and specific ranges for suchparameters, are provided. It should be understood that these areexemplary only, and that others can be used without departing from theintended scope herein.

[0025] The present invention relates to a process and an apparatus forthe process of treating liquid foods and beverages, including, but notlimited to, juices, fruit juices, orange juice, grapefruit juice,tangerine juice, apple juice, stews, and beef stew. The liquid, and, ifany, particulate components, in this system is pressurized anddepressurized to increase the shelf life of the liquid once packaged. Inthe preferred embodiment, the pressure on the liquid (and particulatecomponents, if any) in the system is increased to about 60,000 psig andheld for a sufficient period of time (e.g., about 100 to about 500seconds) to effect the desired kill level of microbial population withinthe liquid. After the liquid food has been pressurized, it is rapidlydepressurized to cause the remaining microbes within the liquid food tofracture. To maintain the integrity and taste of the liquid, thetemperature for the liquid food in the process and the apparatus ismaintained within a desired temperature range, preferably between about35 degrees Fahrenheit and about 85 degrees Fahrenheit.

[0026] Turning now to FIG. 1, a flow chart is provided to illustrate aprocess according to the present invention. The illustrated processinvolves a liquid and a particulate component, it being understood thatthe present invention also applies in cases where there is only a liquidcomponent.

[0027] As illustrated in FIG. 1, the process begins with step A whereinuntreated liquid food of approximately 10% particulate component isintroduced into the pressurized system. The liquid food is thenseparated into a liquid component and a particulate component in step Bvia a separator. The liquid and particulate components are each sent forseparate pressure treatments in steps C and D respectively. Once theliquid and particulate matter have been pressure treated, the twocomponents are blended in step E. Finally, this bulk product is packagedfor storing in step F.

[0028]FIG. 2 illustrates step C of FIG. 1, in which the liquid istreated in a continuous (as opposed to batch) process. Step C1 in thisprocess involves introducing the liquid component into a continuoussystem for the pressurization and depressurization of the liquidcomponent. Next, in step C2, the liquid reaches a first stage in thesystem whereby the pressure on the liquid increases to a first pressure,which may be about 30,000 psig, as the liquid flows through the system.In step C3, the liquid reaches a second stage in the system whereby thepressure on the liquid increases to a second pressure, which may beabout 60,000 psig, as the liquid flows through the system. Pressurizingthe liquid component in two stages facilitates continuous treatment.However, it should be understood that pressure could be increased at asingle stage without departing from the intended scope herein. In stepC4, the liquid component is processed at the second pressure for a timesufficient to affect a desired microbial kill level (for example,between about 100 and 300 seconds). At this pressure, the originalvolume of liquid component is reduced.

[0029] In steps C5-C12 the liquid is introduced into a third stage inthe system whereby volume of the liquid is increased while the pressureon the liquid is reduced to a third pressure, such as atmosphericpressure. In a particular embodiment, the pressure reduction occursthrough a series of steps to keep the liquid within a desiredtemperature range, so as to minimize temperature-induced off-tastes.Exemplary steps are illustrated in C5-C12. It should be understood,however, that more or less (including only one) of these steps may beused without departing from the intended scope herein.

[0030] In step C5 the pressurized liquid in the system is cooled toabout 35 degrees Fahrenheit. Step C6 involves reducing pressure on theliquid to about 41,000 psig, for example, by a reverse Joule-Thompsoneffect, whereby as the pressure in the system reduces and the liquidexpands, the temperature in the liquid increases. Therefore, as thepressure on the liquid is reduced, the temperature of the liquid in thesystem increases, for example, to about 85 degrees Fahrenheit for achange from about 60,000 to about 41,000 psig. Step C7 involves coolingthe liquid again back to 35 degrees Fahrenheit. In step C8, the pressureof the liquid is again reduced, for example, to about 21,000 psig.Again, this causes the temperature of the liquid to increase. Step C9involves cooling the liquid back to 35 degrees Fahrenheit. In step C10,the pressure of the liquid is again reduced to about 1,500 psig. StepC11 involves again cooling the liquid, for example, to 35 degreesFahrenheit. Finally, in step C12, the pressure of the liquid is againreduced, this time to atmospheric pressure. In step C12 the liquidcomponent is then sent to a liquid component and particulate componentmixer, if a particulate component is provided.

[0031] The temperatures, pressures, and times illustrated in the aboveexample, and below, may be changed, depending on the desired costs,temperature sensitivity of the liquid, and other considerations.

[0032] To fully treat the liquid component material in the processdescribed above, there is provided in FIG. 3 a supercritical liquidtreatment apparatus 1. More particularly, FIG. 3 shows a liquidcomponent feed line 10 having a block valve 10 a. Liquid component feedline 10 connects to a liquid feed pump 12 whereby the liquid componentfeeds into liquid feed pump 12 at a temperature of 35 degrees Fahrenheitand a pressure of 20 psig. In addition, connected to line 10 is hotwater line 14 containing valve 14 a located between line 10 and hotwater tank 16. During the treatment of the liquid component, valve 14 aon hot water line 14 is closed. Liquid feed pump 12 increases thepressure of the liquid component to 500 psig and temperature to 37degrees Fahrenheit and pumps the liquid component into line 20. Line 20splits into three separate lines 22, 24 and 26 wherein lines 22 and 24feed into intensifier 30 while line 26 is a release (or surge) line.

[0033] The first intensifier comprises a first cylinder 34 a and asecond cylinder 34 b connected to hydraulic power chambers 36 a and 36 brespectively. Plungers 38 a and 38 b are disposed within cylinders 34 aand 34 b respectively. Hydraulic power package 50 is connected tocylinders 34 a and 34 b via lines 52 and 54 respectively. Lines 52 and54 allow hydraulic fluid to flow from power chambers 36 a and 36 b tohydraulic power package 50 and then back again. Power package 50controls the movement of plungers 38 a and 38 b within cylinders 34 aand 34 b by the flow of hydraulic fluid through valves 56 and 58 locatedwithin power pack 50. The pressure of the hydraulic fluid in lines 52and 54 is between about 1,800 psig and about 3,000 psig.

[0034] For example, pack 50 drives plungers 38 a and 38 b from point Bto point A by simultaneously drawing hydraulic fluid from power chamber36 b and driving hydraulic fluid into power chamber 36 a. As hydraulicfluid enters power chamber 36 a, it drives plunger 38 a through itscompression stroke from point B to point A. Accordingly, as hydraulicfluid leaves power chamber 36 b, plunger 38 b is drawn from point B topoint A and is in its suction stroke. When plungers 38 a and 38 b reachpoint A, valves 56 and 58 in power package 50 reverse themselves causingplungers 38 a and 38 b to reverse direction and move towards position Bwhereby plunger 38 a is now in a suction stroke and plunger 38 b is in acompression stroke.

[0035] To fill the cylinders of intensifier 30 the liquid component ispressurized at 500 psig so it can serve as a positive feed into thecylinders of the intensifier 30 when the plungers in their cylinder arein their suction stroke. For example, the pressurized liquid in processline 22 feeds into first cylinder 34 a when plunger 38 a is in a suctionstroke. In addition, pressurized liquid in process line 24 feeds intocylinder 34 b when plunger 38 b is in a suction stroke.

[0036] To maintain a constant pressure in first intensifier 30, there isprovided a release line 26 connected to process line 20 beforeintensifier 30. Along release line 26 is pressure control valve 26 a.Pressure control valve 26 a is designed so that when pressure insideintensifier 30 exceeds certain pressure, such as about 30,000 psig,pressure control valve 26 a will open, allowing additional liquid toflow down release line 26 and eventually into surge tank 40. The levelof the liquid in surge tank 40 will vary, and an inert ballast gas(e.g., nitrogen) is provided in tank 40 via gas tank 42 which isconnected to surge tank 40 through line 44. The liquid inside surge tank40 may be recycled through the system and back into pump 10 throughrecycling line 46.

[0037] The movement of these plungers in the cylinder through theircompression stroke increase the pressure of the liquid in the system toabout 30,000 psig. Plungers 38 a and 38 b, upon movement through thecompression stroke, force the pressurized liquid, in cylinders 34 a and34 b through lines 70 and 72 respectively, and into surge drum 76. Thepressure on the liquid when it enters surge drum 76 is about 30,000psig, and the increase in pressure on this liquid is also accompanied byan increase in temperature, for about 57 degrees Fahrenheit at about30,000 psig.

[0038] The liquid in surge drum 76 serves as a pressurized feed intoflow line 80. Flow line 80 then splits into lines 84 and 88. Both lines84 and 88 split such that line 84 now continues parallel to line 94, andline 88 continues parallel to line 98. All four lines feed into a secondstage intensifier unit comprising a first intensifier 110 and a secondintensifier 120 connected in parallel with each other. For example,lines 94 and 98 connect to intensifier 110 and lines 84 and 88, runningparallel to lines 94 and 98 respectively, connect to intensifier 120.

[0039] While the present embodiment of the invention discloses a secondstage intensifier unit that comprises two intensifiers 110 and 120connected in parallel with each, other embodiments, for example a singleintensifier, may be used without departing from the intended scopeherein. This parallel design is created to more efficiently handlecapacities greater than 50 gpm and pressures greater than 2750 bar.Furthermore, although the preferred embodiment discussed herein includestwo intensifier stages (intensifier, 30 and second stage intensifierunit (110 and 120)), one pressure increase stage may also be used, forexample with a single intensifier or single intensifier unit of parallelintensifiers.

[0040] Intensifier 110 comprises cylinders 114 a and 114 b for housingplungers 118 a and 118 b while intensifier 120 comprises cylinders 124 aand 124 b for housing plungers 128 a and 128 b. Similar to first stageintensifier 30, the plungers in second stage intensifiers 110 and 120move reciprocal to each other within their respective cylinders. Inaddition, plunger movement in intensifiers 110 and 120 are controlled byhydraulic power pack 130.

[0041] For example, the liquid that flows into second stage intensifier110 leaves surge drum 76, flows through lines 80, then through lines 84and 88 until lines 84 and 88 join lines 94 and 98. The fluid flows intolines 94 and 98 and alternately enters cylinders 114 a, and 114 b, whenplungers 118 a and 118 b are in their suction stroke. Plunger 118 a isin its suction stroke when plungers 118 a and 118 b move from position Ato position B within cylinders 114 a and 114 b. Accordingly, plunger 118b is in its compression stroke. When plungers 118 a and 118 b move backfrom position B to position A plunger 114 b is now in its suction strokewhile plunger 114 a is in its compression stroke.

[0042] For the liquid that flows into second stage intensifier 120, thepressurized liquid leaves surge drum 76, through line 80, next flowsinto lines 84 and 88, and enters cylinders 124 a, and 124 b whenplungers 128 a and 128 b are in their suction stroke. Plunger 128 a isin its suction stroke when plungers 128 a and 128 b move from position Ato position B within cylinders 124 a and 124 b. Accordingly, plunger 128b is in its compression stroke. When plungers 128 a and 128 b move backfrom position B to position A, plunger 128 b is now in its suctionstroke while plunger 128 a is in its compression stroke.

[0043] Hydraulic power pack 130 controls the flow of the plungers insidesecond stage intensifiers 110 and 120. Lines 142 and 144 connecthydraulic power pack 130 to power chambers 116 a and 116 b, while lines146 and 148 connect hydraulic power pack 130 to power chambers 126 a and126 b. The pressure of the hydraulic fluid in lines 142, 144, 146 and148 is between about 1,800 psig and about 3,000 psig. As disclosedabove, hydraulic power pack 130 controls the movement of the plungers inthe cylinders such that when a compression stroke is completed, valves132 and 134 in hydraulic power pack 130, are reversed causing theintensifier plungers to move in the opposite direction.

[0044] Second stage intensifiers 110 and 120 increase the pressure ofthe liquid to about 60,000 psig. This increase in pressure will alsoresult in the liquid increasing in temperature to approximately 83degrees Fahrenheit.

[0045] Plungers 118 a and 118 b alternately force the discharge of thecompressed liquid through lines 160 and 162 during their compressionstroke. Similarly, plungers 128 a and 128 b alternately force thecompressed liquid through lines 170 and 172 during the compressionstroke of plungers 128 a and 128 b. Lines 160 and 162 then meet and formline 166 while lines 170 and 172 meet and form line 176. Lines 166 and176 then join line 180.

[0046] The system may require periodic maintenance, therefore, anadditional embodiment of the invention is shown in FIG. 4 whereby theliquid component treatment system is provided with a supplementalmaintenance control system. This system is similar to the systemdescribed in FIG. 3 however, this system contains an additional seriesof lines and block valves. For example, the system contains anadditional line 200 which connects to line 20 before valve 20 a on line20. Line 200 extends from line 20 and connects to lines 94 and 98. Line200 contains valves 200 a and 200 b with valve 200 a located betweenline 20 and line 94 and valve 200 b located between line 94 and line 98.In addition the system is provided with a Line 210 which connects tosurge drum 76 and extends to line 166. Line 210 contains valves 210 aand 210 b.

[0047] This system also contains an additional series of block valves.For example, lines 70 and 72 contain valves 70 a and 72 a respectively.Lines 84 and 94 contain valves 84 a and 94 a located on their respectivelines after line 94 separates from line 84. Similarly, lines 88 and 98contain valves 88 a and 98 a located on their respective lines afterline 98 separates from line 88. Lines 142, 144, 146 and 148 containvalves 142 a, 144 a, 146 a, and 148 a respectively. Line 166 containsvalve 166 a between line 210 and line 180. Line 180 contains valve 180 abetween line 176 and line 166.

[0048] These additional lines and valves can be opened or closed toallow a series of repairs to intensifiers 30, 110 and 120. During normaloperating conditions, valves 200 a, 200 b on line 200. and 210 a and 210b on line 210 are closed while all other valves are open. However, whenit is necessary to repair intensifier 110, valves 94 a and 98 a areclosed preventing the liquid component from flowing through lines 94 and98 and into intensifier 110. In addition, valves 142 a and 144 a onlines 142 and 144 are closed preventing hydraulic fluid from flowingfrom intensifier 130 into hydraulic chambers 116 a and 116 b. Theclosure of these valves then frees intensifier 110 to be repaired whilethe system is still running.

[0049] When repairs to intensifier 120 are necessary, valves 84 a and 88a are closed, preventing the liquid component from flowing through lines84 and 88 and into intensifier 120. In addition, valves 146 a and 148 aare closed on lines 146 and 148 preventing hydraulic fluid from flowingfrom intensifier 130 into hydraulic chambers 126 a and 126 b. Theclosure of these valves then leaves intensifier 120 free to be repairedwhile the system is still running.

[0050] When it is necessary to repair intensifier 30, valve 20 a isclosed and valves 200 a and 200 b are opened to allow fluid into line200 of the system. The fluid then feeds alternatively into lines 94 and98 and then into cylinders 114 a and 114 b of intensifier 110 duringtheir suction stroke. The pressurized liquid flows into lines 160 and162 and then flows into line 166. Line 166 joins line 210 whereby whenvalves 210 a and 210 b on line 210 are open and valve 166 a on line 166is closed, the fluid flows into surge drum 76. Valves 70 a and 72 a areclosed to prevent flow of the liquid component from surge drum 76 intolines 70 and 72. The fluid in surge drum 76 then serves as a pressurizedfeed into intensifier 120. This is because valves 94 a and 98 a on lines94 and 98 are closed preventing the fluid from flowing into intensifier110. This situation then leaves intensifier 30 free to be repaired whilethe system is still running.

[0051] Once the liquid component is pressurized, for example to about60,000 psig, by intensifiers 110 and 120, it is fed through lines 166and 176 into line 180. Line 180 then meets tubular receiver 220. Insidetubular receiver 220, the liquid is maintained at the elevated pressurewhere a portion of the microorganisms are killed by being maintainedunder a high pressure for a sufficient period of time (e.g. about 100 toabout 500 seconds). To keep this treatment process continuous, the flowof the liquid is continuous through the tubular receiver. The length ofthe tubular receiver will depend on, among other things, flow rates,dimensions, and the amount of the time needed for the desired killlevel. The times provided herein may be lengthened, or shortened,depending on, among other things, initial microbial levels and desiredkill levels.

[0052] As shown in FIG. 5, receiver 220 can be of autoclave or tubulardesign, and will be of a compound construction with an outer pressuretubing 222 and a thin wall liner of corrosion resistant stainless steel224. Outer pressure tubing 222 comprises ASTM standard 4340 steel withan inner bore face 222 a having a diameter about 2.5 inches and outerface 222 b having a diameter measuring about 6.5 inches, however anycomposition of pressure tubing meeting the strength requirements may beused.

[0053] Inner liner 224 may consist of Type 304 stainless steel tubinghaving inner bore surface 224 a having a diameter measuringapproximately 2.0 inches, and outer surface 224 b having a diametermeasuring 2.375 inches. Inner liner 224 will be slipped inside of innerbore 222 a of outer pressure tubing 222 and will be hydraulicallyexpanded via an autofrettage process to tight fit to the 2.5 inch insidediameter of bore 222 a. The purpose of the stainless steel liner is toprovide corrosion resistance against the PH of the liquid being treatedand to be compatible with the requirements of food processing.

[0054] The system may also be provided with safety mechanisms to preventthe rupture or tear of any of the lines or components within the system,therefore an additional embodiment of the invention is shown in FIG. 6.FIG. 6 discloses a rupture disk 212 attached to line 72 before line 72connects to surge drum 76. Rupture disk 212 is set to rupture at about40,000 psig and thereby warning any operator of the system that thepressure of the liquid component in line 72 or surge tank 76 hasexceeded about 40,000 psig. In addition, another rupture disk 214 isconnected to line 180 as line 166 joins line 180. Rupture disk 214 isset to rupture at about 65,000 psig and thereby warning any operator ofthe system that the pressure of the liquid component in line 180 hasexceeded about 65,000 psig. Line 180 then connects to tubular receiver220. On the other side of tubular receiver 220, is line 228 connectedthereto. Connected to line 228 is automatic shutdown controller 229which shuts the system down if the pressure in the system breaks eitherrupture disk.

[0055] As shown in FIG. 3 Line 228 connects to heat exchanger 230. Thisheat exchanger reduces the temperature of the pressurized liquid fromabout 83 degrees Fahrenheit to about 35 degrees Fahrenheit. In addition,connected to line 228 is pressure let down station 240 as shown in FIG.7. Pressure let-down station 240 actually consists of an alternatingseries of pressure let-down controllers 242 a, 242 b, 242 c each in analternating series with heat exchangers 244 a, 244 b, and 244 c followedby pressure control valve 248 which combine to reduce the pressure inthe liquid to atmospheric pressure by a series of steps while keepingthe temperature of the liquid component at or below about 85 degreesFahrenheit. Line 228 links the pressure let down controllers to the heatexchangers in this series.

[0056] Pressure let down controllers 242 a, 242 b, and 242 c eachcomprise a pressure control valve 260 (FIG. 8) and a flow controlorifice 280 (FIG. 9). FIG. 8 shows that pressure control valve 260 iscomprised of a valve body 262, with valve stem 264 housed within thevalve body 262. Valve stem 264 is secured within valve body 262 by gland266 and valve stem 264 is supported inside valve body 262 by packing268.

[0057] Valve seat 269 rests against valve stem 264 inside valve body262. The lines in the system are made up of pressure tubing 222 andliner 224 which rests against valve seat 269 inside valve body 262.Pressure tubing 222 and liner 224 are secured within valve body 262 byclamping block 274 and bolts 276 and 278 which secure clamping block 274to valve body 262.

[0058]FIG. 9 shows the cross sectional view of flow control orifice 280which is spliced between two sections of pressure tubing 222 and liner224 which ultimately form line 228. Flow control orifice comprises twohubs 282 and 284 which are threaded around pressure tubing 222. Clamps286 and 288 clamp hubs 282 and 284 together and force both ends ofpressure tubing line 228 into collar 290. Collar 290 supports sapphireorifice 291 and gland 292 which is threaded into collar 290 aftersapphire orifice 291. The minimum diameter of this flow control orifice280 is about 0.2 inches which is large enough to pass any particulatewhat may be flushed out during a clean-in-place washing of the processequipment.

[0059] The design of the orifice controller and the downstream tubing issuch that at the discharge of the orifices, eddies are createddownstream of the orifice with the eddies assisting in the absorption ofthe kinetic energy of the jet stream.

[0060] Maintenance or replacement of an orifice may be required fromtime to time. Therefore, the installation of double block valves may beprovided within the system just prior to the pressure let down stationto periodically replace certain sections of the system without reducingthe pressure in the system. It is important to maintain a constantpressure in this system to avoid a cycling of the system which mayresult in a shorter life of the components.

[0061] While the liquid component is compressed in tubular receiver 220,the pressure in the system reduces the liquid component to about 87.5%of its original volume. When the liquid component reaches the pressurelet down stage, it is expanded to its original volume through a seriesof steps. In this case, the expansion of the liquid occurs through areverse Joule-Thompson effect, whereby the liquid will heat up duringeach pressure let down step. To maintain the quality of the liquid (e.g.orange juice) in the apparatus, the heat exchanger following eachpressure relief valve will keep the temperature of the liquid belowabout 85 degrees Fahrenheit. Thermodynamically, the expansion acrosseach pressure let-down controller is shown in FIG. 10.

[0062] For example, the cooled liquid component enters pressure let downcontroller 242 a with a temperature of about 35 degrees Fahrenheit and apressure of about 60,000 psig. Pressure let down controllersimultaneously decreases the pressure of the liquid to about 41,000while increasing the temperature to about 85 degrees Fahrenheit. Theliquid then enters heat exchanger 244 a where it is cooled back to atemperature of about 35 degrees Fahrenheit. The liquid then enterspressure let down controllers 242 b. Pressure let down valvesimultaneously decreases the pressure of the liquid to about 21,000while increasing the temperature of the liquid to about 85 degreesFahrenheit. Heat exchanger 244 b then cools the liquid back to about 35degrees Fahrenheit. Next, the liquid enters pressure let down controller242 c where the pressure is further reduced to about 1,500 psig whilethe liquid again heats up to about 85 degrees Fahrenheit. Heat exchanger244 c cools the liquid back to about 35 degrees Fahrenheit. While thefirst three pressure reductions work under the reverse Joule ThompsonEffect the last pressure reduction does not. Accordingly, when theliquid enters pressure control valve 248 the pressure is reduced toabout 14.5 psig without any noticeable temperature increase. The flowrates across pressure let down controllers 242 a, 242 b, and 242 c areabout 2,000 ft/sec, about 1,500 ft/sec, and about 1,000 ft/secrespectively. These flow rates across the pressure let down controllersare sufficient to cause the remaining microorganisms within the liquidcomponent to fracture and thereby facilitate the sterilization of theliquid component.

[0063] The liquid component then moves down line 228 and into mixing tee293 (FIG. 7). Mixing tee 293 connects to line 294 which then splits intolines 295 and 296 having valves 295 a and 296 a respectively. Inaddition, mixing tee 293 connects to pulp slurry line 297. Pulp slurryline 297 has valve 297 a and connects to pulp slurry pump 298. Pulpslurry pump 298 is fed by pulp slurry line 299. Therefore, the liquidcomponent mixes with the particulate component in mixing tee 297 andthen flows to packaging down line 294 and then down line 296.

[0064] In following with the standards of the industry, the highpressure liquid treatment system may be periodically flushed, with asolvent (e.g. hot water) to remove the build-up of any particulate orcoatings of components by the liquid food. The solvent can be an acidwash but it should be chemically compatible with the equipment. To avoidunnecessary cycling in the system, the operating pressures within thesystem are maintained while the fluid feed in the system is changed overfrom the liquid component of liquid food to a solvent. Therefore, toflush the system of particulates, valve 10 a on line 10 (FIG. 2) isclosed while valve 14 a on line 14 is opened. This step stops the flowof the liquid component into the system, and allows a solvent or in thiscase, hot water to feed into the system. Hot water feeds into the systemat 180 degrees Fahrenheit and 20 psig into line 14 from hot water tank16. Using standard or above standard operating pressures, the hot wateris pumped through the system to free particulates from the system. Thewater flows through the system by the same process as described abovefor the liquid component of the untreated liquid food. Liquid componenttreatment system 1 has a volume of approximately 400 gallons. Tocompletely flush the system of particulates, it is necessary to flush upto eight volumes of hot water through the system before normalactivities can resume. To avoid having hot water contaminate thepackaging system, valves 295 a and 297 on line 295 and 297 respectivelyare closed while valve 296 a on line 296 is opened to allow the hotwater treatment to flow through the system and down line 296 instead ofline 295. The system may be flushed with hot water once every 24 hoursand then returned back to treating the liquid component of the liquidfood.

[0065] Sterilizing the Particulate Component

[0066]FIG. 11 discloses the batch process for sterilizing theparticulate component of the liquid food as shown in step D of FIG. 1.Although this batch process is described in connection with theparticulate component, the liquid component can also be treated withthis batch process, alone or in combination with the previouslydescribed continuous process.

[0067] Step D1 involves introducing the particulate component into apressurized system. In Step D2, the pressure on particulate component inthe system is increased to about 40,000 psig to about 60,000 psigwhereby the temperature of the particulate component in the system willincrease by approximately 20 degrees Fahrenheit. Next, step D3 involvesholding the particulate component at a constant pressure for aproscribed period of time (e.g. about 100 to about 300 seconds) whichwill sterilize the particulate component by killing off microorganismsin the particulate component. Step D4 involves rapidly reducing thepressure on the particulate component to atmospheric pressure. Duringthis rapid pressure reduction step, a portion of the liquid particulatecomponent may reach temperatures as high as about 240 degrees Fahrenheitand maintain an average temperature of about 125 degrees Fahrenheit thusexceeding the desired temperature range for the product. Another portionof the particulate component will remain within the desired temperaturerange of about 35 to about 85 degrees Fahrenheit. Therefore, step D5involves separating the high temperature particulate component from thelow temperature component. In step D6 the high temperature liquidparticulate component is transferred to an off site tank. Next, step D7involves transferring the treated low temperature particulate componentproduct to a liquid component and particulate component mixer.

[0068] To fully treat the particulate component in the process describedabove, the particulate component is sent to a particulate treatmentsystem 300. This system may be comprised of a single receiver treatmentsystem 310 in FIG. 12 or a double receiver treatment system 400 in FIG.13. In either of these systems, the particulate component of the liquidis held at an elevated pressure of about 60,000 psig for a proscribedlength of time (e.g. about 100 to about 300 seconds) to deactivatemicroorganisms that may be present in the particulate component.

[0069]FIG. 12 shows the single receiver system 310. This high pressureparticulate system comprises a series of lines 312, 314, 316, 318, 320,322 and 324 which connect feed tank 330, intensifier 340, bleed tank350, product tank 360, and receiver 370 together and allow theparticulate component to flow between them.

[0070] Line 312 which comprises valve 312 a and temperature gauge 312 bconnects feed tank 330 to receiver 370. Line 314 which comprises valve314 a connects product tank 360 to line 312 between valve 312 a andreceiver 370. Vent line 316 extends from receiver 370 and containspressure gauge 316 a, valve 316 b, and pressure control valve 316 c.Nitrogen line 318 contains pressure control valve 318 a, and valve 318 band connects to vent line between valve 316 b and receiver 370. Line 320which comprises temperature gauge 320 a, pressure gauge 320 b and valve320 c, connects intensifier 340 to line 316 between valve 316 b andreceiver 370. Line 322 includes valve 322 a, temperature gauge 322 b andvalve 322 c connects bleed tank 350 to vent line 316 between valve 316 band receiver 370. Line 324 connects to intensifier 340 to allowpressurizing liquid to flow into intensifier 340.

[0071] Included in this sterilizing system 310 is a system of blanketinggas which is used in all tanks to protect the particulate component fromoxidation. Blanketing gas pressure can also be used as a motive force toassist the gravity flow of the particulate component from one tank toanother. In the single receiver configuration 310 (FIG. 12), each vesselhas a separate source of chemical grade nitrogen and a pressure ventvalve. In the multi-receiver configuration 400 (FIG. 13), each tank andreceiver has a dedicated nitrogen system for blanketing gas and gasassisted feed and product transfers.

[0072] For example, connected to feed tank 330 is feed line 332 havingvalve 332 a, and vent line 334 having pressure control valve 334 a. Ventline 334 connects to nitrogen line 336 having pressure control valve 336a. Pressure control line 337 connects pressure control valve 334 a onvent line 334 to pressure control valve 336 a on nitrogen line 336.Also, connected to feed tank 330 is pressure gauge 338 and temperaturegauge 339 for reading the pressure and temperature of the particulatematter in the feed tank.

[0073] Connected to bleed tank 350 is product line 352 having valve 352a and vent line 354 having pressure control valve 354 a. Vent line 354connects to nitrogen line 356 having pressure control valve 356 a.Pressure control line 357 connects pressure valve 354 a on vent line 354to pressure control valve 356 a on nitrogen line 356. Also connected tobleed tank 350 is pressure gauge 358 and temperature gauge 359 forreading the pressure and temperature in the bleed tank.

[0074] Connected to product tank 360 is product line 299 (FIG. 2) havingvalve 299 a, and vent line 364, having pressure control valve 364 a.Vent line 364 connects to nitrogen line 366 having pressure controlvalve 366 a. Pressure control line 367 connects pressure control valve364 a on vent line 364 to pressure control valve 366 a on nitrogen line366. Also connected to product tank 360 is pressure gauge 368 andtemperature gauge 369 for reading the pressure and temperature in thebleed tank.

[0075] Receiver 370 as shown in FIGS. 12 and 14 includes temperaturecontrol gauge 372, connected to thermocouple 374 which is housed withintubing 376. In addition, conductivity cell 378 is located withinreceiver 370 to detect whether receiver 370 has filled with particulatecomponent. As shown in FIG. 14 a cross-sectional representation ofreceiver 370 shows the receiver itself comprises an outer casing 380,and an inner casing 382. Inner casing 382 has an inner wall 382 a and anouter wall 382 b. Inner casing 382 is substantially cylindrical inshape, but it angles in at a 45 degree angle at both a bottom end 384,and a top end 386. Both bottom end 384 and top end 386 taper to ducts388 and 390 respectively. Bottom end 384 is supported within outercasino 380 by bottom plug 392. Top end 386 is supported within outercasino 380 by top plug 394.

[0076] To process the particulate component using the system 310, bulkuntreated particulate component slurry is fed into elevated feed tank330. The slurry has a concentration in the range of 40% to 60% andpreferably about 50% particulate matter with the balance being anuntreated liquid component. This concentration of approximately 50% pulpand 50% liquid facilitates reasonably rapid transfers of the slurry fromtank to tank. Other less or more concentrated slurries of particulatematter can be used, with more concentrated particulate slurriesrequiring positive displacement. This mixture is fed through feed line332 into feed tank 330. As feed tank 330 fills, nitrogen blanketing gasleaves feed tank 330, and vents through line 334. As the untreatedmixture leaves feed tank 330, nitrogen blanketing gas is then fed backinto feed tank 330 via nitrogen line 336.

[0077] The untreated mixture is fed by gravity flow out of feed tank 330through line 312 and into a lower end of receiver 370, filling receiver370 from the bottom up. To prevent any degradation of the particulatecomponent, receiver 370 is filled with a blanketing gas (preferablynitrogen) that is displaced out of receiver 370 as the tank is filledwith particulate matter. The displaced nitrogen gas from receiver 370flows through line 316 to vent. When the receiver is completely full, asindicated by conductivity cell 378, or other suitable means, flow fromthe particulate component is stopped by closing valve 312 a in line 312.Valves 316 b in line 316, and 322 a in line 322 are then closed. Anuntreated liquid component is introduced into the system via line 324.The untreated liquid is next pumped through intensifier 340 and placedinto line 320. The liquid feeds into receiver 370 and the receiver ispressurized by intensifier 340 forcing the liquid component through thesystem. The system is then pressurized by intensifier 340 between about40,000 and about 60,000 psig. When the intensifier discharge pressureand the receiver pressure reaches its target pressure the pressurizationis discontinued, and valve 320 c in line 320 is closed. Duringpressurization, the temperature of the particulate component in thereceiver will increase slightly (e.g. by about 20 degrees Fahrenheit).The liquid in the filled and pressurized receiver is then allowed tostand, under pressure, for a prescribed residence time (e.g. about 100to about 300 seconds) which will cause the deactivation of themicroorganisms in the pressurized slurry of particulate and liquidcomponent.

[0078] After expiration of the prescribed residence time (e.g. up toabout 300 seconds), valves 322 a and 322 c in line 322 are opened,allowing the pressure in receiver 370 to be vented to bleed tank 350.This vented liquid slurry, being the last used to pressurize thereceiver, causes the pressure in the receiver to be rapidly reduced toessentially atmospheric pressure. The pressure drop is via isenthalpicexpansion, causing the initial temperature of the vented fluid to reachtemperatures as high as about 240 degrees Fahrenheit. The temperature ofthe vented liquid will gradually decrease as the pressure in the ventedreceiver decreases, dropping to about 50 degrees Fahrenheit at the endof the depressurization. However, the average temperature of the ventedliquid stream is about 125 degrees Fahrenheit, exceeding its maximumallowed temperature. The liquid accumulated in bleed tank 350 havingexceeded the maximum allowable temperature, is therefore designed aslower valued premium product and is transferred to an off-site tank forlater use in a lesser valued product.

[0079] The treated particulate component slurry is discharged fromreceiver 370 to product tank 360 by opening valve 314 a on line 314 andallowing fresh blanketing gas from nitrogen line 318 to displace thelost volume in receiver 370. The rate of transfer may be accelerated byincreasing the pressure of the blanketing nitrogen gas. As the slurryflows into product tank 360, the displaced blanketing gas in producttank 360 vents to the atmosphere via vent line 364. Next, theparticulate component flows down line 299 to mix with the liquidcomponent (FIG. 2). No mixer is needed if the liquid component istreated with the batch process alone.

[0080] As an example of this process, using a 16″×81″ receiver, five 700lb batches of particulate component (e.g. pulp) each containing about350 lb of both liquid food and particulate component can be deactivatedper hour. The cycle time of about 12 minutes per batch includes the timefor charging the receiver, pressurizing it, holding it for a prescribedresidence time, venting the pressure and transferring the treatedproduct to product tank 360. The transfer times may be altered bychanging the viscosity of the particulate component or by using anitrogen gas assist. Altering the viscosity can be done by an increaseor a reduction of the liquid content of the particulate component.

[0081] Each 700 lb batch of particulate component slurry will processabout 350 pounds of particulate component (e.g. pulp), which willproduce about 3500 lb/hr, or about 401 gallon/hr of final brix 12blended product. The above dimensioned single reactor configuration willproduce about 1,750 lb, of particulate component/hour compared to a needfor about 6,282 lbs/hr to process about 100 gpm of liquid component(e.g. juice). Thus, to meet the higher capacity liquid componenttreatment system, either the size of the receiver must be increased oradditional receivers must be installed.

[0082] Multi-Receiver Configuration

[0083] The multi-receiver system 400 (FIG. 13) differs from the singlereceiver system in that the multi-receiver system contains an additionalreceiver 402 and a different set of lines connecting feed tank 330,intensifier 340, bleed tank 350, product tank 360 to first receiver 370,and second receiver 402. In the multi-receiver system, line 410 containspressure valve 410 a and connects feed tank 330 to intensifier 340. Inaddition, connected to line 410 are lines 412 and 414 which connect line410 to receiver lines 416 and 418 respectively. Line 412 contains valve412 a while line 414 contains valve 414 a. Receiver line 416 extendsfrom receiver 370 to product line 420 and comprises valves 416 a and 416b connected to receiver line 416 on either side of line 412. Inaddition, receiver line 418 extends from receiver 402 to product line422 and contains valves 418 a and 418 b located on line 418 on eitherside of line 414. Product line 420 feeds into product line 422 whereinproduct line 422 then feeds into product tank 360.

[0084] Line 430 extends from intensifier 340 and contains temperaturegauge 430 a. Line 430 splits into two lines 434 and 438. Line 434contains valve 434 a and pressure gauge 434 b and connects line 430 toreceiver line 440. Line 438 contains valve 438 a and pressure gauge 434b and connects line 430 to receiver line 442. Receiver line 440 andreceiver line 442 connect to receiver 370 and receiver 380 respectively.Receiver line 440 contains first pressure valve 440 a, second pressurevalve 440 b, and pressure control valve 440 c. Receiver line 442contains first pressure valve 442 a, second pressure valve 442 b andpressure control valve 442 c. Line 450 connects receiver lines 440 and442 and contains a first valve 450 a, a first pressure control valve 450b, a second pressure control valve 450 c and a second valve 450 d. Inaddition, connected to line 450 between pressure control valve 450 b and450 c is nitrogen input line 452.

[0085] Line 460 connects receiver lines 440 and 442 to bleed tank 350.Line 460 contains valve 460 a, temperature gauge 460 b, and valve 460 c.Valve 460 a is located between receiver lines 440 and 442, whiletemperature gauge 460 b and valve 460 c are located on line 460 betweenreceiver line 442 and bleed tank 350.

[0086] The dual receiver operation starts when the untreated particulatecomponent leaves elevated feed tank 330 and travels down line 410 bygravity through line 412, entering line 416 where it flows into firstreceiver 370. Valve 410 a is closed preventing particulate componentfrom entering intensifier 340. As the particulate component enters thebottom of receiver 370, nitrogen blanketing as leaves receiver 370 andvents through line 440. When receiver 370 fills to the top, valves 412a, 416 a, and 440 a close. Once receiver 370 is full its pressure isincreased with raw particulate component (e.g. pulp) from feed tank 330.Valve 410 a opens and the raw particulate component flows from feed tank330 though line 410 and into intensifier 340. Intensifier 340 pumps theparticulate component into line 430, through line 434, and into receiver370. During pressurization to the deactivation pressure, the temperatureof the particulate component in receiver 370 will reach about 51 degreesFahrenheit which is well within the preferred product temperature rangeof about 35 degrees Fahrenheit to about 85 degrees Fahrenheit. Afterreceiver 370 reaches its target treatment pressure, the flow fromintensifier 340 is stopped and valve 434 a is closed to lock theparticulate component in receiver 370 for a treatment time of 100 to 300seconds at a pressure between about 40,000 to about 60,000 psig.

[0087] As the first receiver tank 370 sterilizes a batch, valve 410 acloses but valve 414 a opens to allow an additional batch to flow bygravity from feed tank 330 into line 414, next into line 418, flowinginto the bottom of second receiver 402. As second receiver 402 fillswith the particulate component, nitrogen blanketing gas leaves receiver402 and vents through line 442. When receiver 402 fills to the top,valves 414 a, 418 a and 442 a close. Once receiver 402 is full, itspressure is increased with raw particulate component (e.g. pulp) fromfeed tank 330. Valve 410 a now opens allowing the raw particulatecomponent from feed tank 330 to flow through line 410 and intointensifier 340. Intensifier 340 pumps the particulate component throughline 430, into line 438 and then into the top of receiver 402. Duringpressurization to the deactivation pressure, the temperature of theparticulate component in receiver 402 will reach approximately 51degrees Fahrenheit which is well within the product temperature range ofabout 35 degrees Fahrenheit to about 85 degrees Fahrenheit. Afterreceiver 402 reaches its target treatment pressure, the flow fromintensifier 340 is stopped and valve 438 a is closed to lock theparticulate component in receiver 402 for a treatment time of about 100to about 300 seconds at a pressure between about 40,000 and about 60,000psig.

[0088] Once second receiver 402 is pressurized to the deactivationpressure, the procedure for discharging treated particulate componentfrom receiver 370 is started. The pressure in receiver 370 is reducedfrom about 60,000 psig to atmospheric by venting the receiver pressurevia lines 460 and 462 to bleed tank 350. This is achieved by openingvalves 440 a, and 460 a, on lines 440, and 460 respectively. In thepressure let down stage, the temperature of the vented stream will reach240 degrees Fahrenheit making it unsuitable for use as a premium blendstock. The temperature of the treated particulate component in receiver370 as measured by the bottom mounted thermocouple settles at about 38degrees Fahrenheit after depressurization. The treated particulatecomponent in receiver 370 is also at about 38 degrees Fahrenheit. Next,valves 416 a and 416 b on line 416 now open and allow the treatedparticulate component to flow through lines 416, 420 and 422 to producttank 360 by gravity, or a possible blanketing gas (e.g. nitrogen)assist. During this transfer, receiver 370 is refilled with blanket gas(e.g. nitrogen). After emptying receiver 370, the system is ready forrefilling again with raw untreated particulate component.

[0089] During the pressure treatment of the second batch particulatecomponent in receiver 370, the cycle starts over again with the drainingand refilling of receiver 402. As in the draining of receiver 370, thepressure in receiver 402 is reduced from about 60,000 psig toatmospheric by venting the receiver pressure via lines 442, and 460 tobleed tank 350. This is achieved by opening valve 442 a in line 442. Thetemperature of the vented steam can reach about 240 degrees Fahrenheitmaking it unsuitable for premium blend stock. However, the temperatureof the treated particulate component in receiver 402 remains at about 38degrees Fahrenheit after depressurization. Next, valves 418 a and 418 bon line 418 open and allow this treated particulate component to flowthrough lines 418 and 422 to product tank 360 by gravity with a possibleblanketing gas (e.g. nitrogen gas) assist.

[0090] Like the single receiver configuration, the multi-receiverconfiguration also utilizes a system blanketing gas (e.g. nitrogen) sothat at no time are the vessels and piping exposed to atmosphericcontamination or oxidizing atmospheres.

[0091] The dimensions and capacity of the receiver configurations can bevaried with a change in internal diameter or length of the receiver andthe tensile strength of the steel, as equipment or process costsdictate.

[0092] In another embodiment of the invention the particulate componentmay be treated in a multi-receiver system using more than two receiversfor processing. If two or more receiver vessels are used, then eachreceiver vessel is filled alternately such that as one receiver vesselis pressurized, the other receiver vessel is being depressurized andrefilled with the next batch.

[0093] The lines in the system are comprised of short segments ofpressure tubing 222 to allow periodic replacement of the lines in thesystem, short segments of pressure tubing 222 are coupled together usinga greylock coupling 500 as shown in FIG. 15. FIG. 15 shows a crosssectional view of greylock coupling 500 which comprises two hubs 510 and520 coupled together by clamps 530 and 540 having bolts 532 and 534 onclamp 530 and bolts 542 and 544 on clamp 540. Hubs 510 and 520 threadonto each end of spliced pressure tubing 222. Seal ring 550 fits betweenthe two spliced ends of pressure tubing 222 and inner liner 224. The twoends of pressure tubing 222 and liner 224 are joined together to formlines in the system by placing clamps 530 and 540 around hubs 510 and520. Bolts 532 and 534 are tightened on clamp 530 to secure clamp 530 tohubs 510 and 520. Bolts 542 and 544 are tightened on clamp 540 to secureclamp 540 to hubs 510 and 520. The tightening of these bolts brings thetwo pieces of pressure tubing together to form a tight seal around sealring 550. If it is necessary to remove a piece of pressure tubing from aline, then bolts 532 and 534 are loosened on clamp 530 and bolts 542 and544 are loosened on clamp 540, allowing pressure tubing 222, whichhouses liner 224, to be removed from the line.

[0094] To close off a line, FIGS. 16 and 17 disclose a cross sectionalview of pressurization end plugs having two different designs. In bothdesigns there is a coupling 610 threaded around pressure tubing 222.Coupling 610 comprises a flange bolt hole 614 and a flange 618. An endportion of pressure tubing 222 is cut away to allow ring 620, housedwithin coupling 610 to contact inner liner 224.

[0095] In the first design, plug 640 (FIG. 16) has a stopper portion 642and a threaded portion 648. Threaded portion 648 threads within coupling610 and stopper portion 642 fits within inner liner 224. Notch 650 iscut within stopper portion 642 with notch 650 for housing ring 652. Plug640 has a inner channel 660 which leads to pressure ring 662. Abovepressure ring 662 is an open channel 664.

[0096] In the second design, plug 670 (FIG. 17) has a stopper portion672 and a threaded portion 678. Threaded portion 678 threads withincoupling 610 and stopper portion 672 fits within inner liner 224. Notch680 is cut within stopper portion 672 with notch 680 for housing ring682.

[0097] The liquid of this process may be, among other things, orangejuice. The pressure vessels and the intensifier discharge lines shouldbe fabricated from high pressure metal alloys such as 4340, 13-8PH,15-5PH, and 17-48 PH precipitation hardened steels. The high pressurevessels and lines are lined with stainless steel to protect the qualityof the product and to preclude corrosion by the pH of the liquid orparticulate component. The low pressure tanks, transfer lines and valvesare fabricated of stainless steel to protect the quality of the productand to preclude corrosion of the hardware.

[0098] Although the present invention has been described in detail, itshould be understood that various modifications, alterations, andsubstitutions can be made to this description without departing fromintended scope of the present invention as defined by the appendedclaims.

What is claimed is:
 1. A process for sterilization of a liquid in acontinuous system comprising: a) substantially continuously pumping theliquid through a pressurized system; b) increasing the pressure of theliquid at a plurality of pressurization stages; c) maintaining theliquid at an elevated pressure for a predetermined period of time; andd) depressurizing the liquid to fracture microorganisms within theliquid.
 2. The process of claim 1 , wherein increasing the pressurecomprises introducing the liquid into an intensifier.
 3. The process ofclaim 1 , wherein the liquid is maintained at the elevated pressure forat least 100 seconds.
 4. The processor of claim 1 , wherein pressure isincreased at two stages.
 5. The process of claim 1 whereindepressurizing the liquid comprises a plurality of pressure reductions.6. The process of claim 1 wherein depressurizing the liquid comprises:reducing the pressure in the liquid from about 60,000 psig to about41,000 psig; reducing the pressure in the liquid from about 41,000 psigto about 21,000 psig; reducing the pressure in the liquid from about21,000 psig to about 1,500 psig; and reducing the pressure in the liquidfrom about 1,500 psig to about 15 psig.
 7. The process of claim 1 andfurther comprising maintaining the temperature of the liquid betweenabout 35 degrees Fahrenheit and about 85 degrees Fahrenheit.
 8. Theprocess of claim 1 further comprising separating the liquid from aparticulate component.
 9. The process of claim 8 further comprising: a)treating the particulate component in a pressurized system by: i)increasing the pressure on the particulate component; and ii) returningthe particulate matter to substantially atmospheric pressure; and b)blending the particulate component with the liquid component.
 10. Theprocess of claim 9 wherein in step i) the particulate component istreated in a plurality of receiver vessels.
 11. An apparatus for thecontinuous sterilization of a liquid in a pressurized system comprising:a pump for continuously introducing the liquid into the pressurizedsystem; a first stage intensifier coupled to the pump, the first stageintensifier for increasing the pressure of the liquid in the system; asecond stage intensifier coupled to the front stage intensifier, thesecond stage intensifier for receiving and increasing the pressure ofthe pressurized liquid in the system; a pressure receiver coupled to thesecond intensifier, the pressure receiver for receiving the pressurizedliquid from the second stage intensifier and maintaining the pressurizedliquid for a predetermined period of time; and a pressure reducercoupled to the pressure receiver wherein the pressure reducer reducesthe pressure of the liquid in the pressurized system to a predeterminedlevel.
 12. The apparatus of claim 11 , wherein the first intensifier hasa plurality of plungers and a plurality of cylinders, the plungers beingreciprocally mounted in the cylinders:
 13. The apparatus of claim 11 ,wherein the second intensifier comprises a plurality of intensifiersconnected in parallel with each other.
 14. The apparatus of claim 11 ,further comprising a surge tank coupled to the first intensifier, thesurge tank for receiving and holding the pressurized liquid from thefirst intensifier.
 15. The apparatus of claim 11 , further comprising asurge tank coupled to the first stage intensifier for recycling aportion of the liquid component before feeding into the first stageintensifier.
 16. The apparatus of claim 11 , wherein the pressurereducer comprises an alternating series of heat exchangers and pressurecontrollers.
 17. The apparatus of claim 11 , wherein the heat exchangersmaintain the temperature of the liquid between about 35 degreesFahrenheit and about 85 degrees Fahrenheit.
 18. The apparatus as inclaim 11 , further comprising a liquid component and particulatecomponent separator connected to the liquid pump for separatingparticles from the liquid.
 19. The apparatus as in claim 18 , furthercomprising a particulate treatment apparatus coupled to the separator,the treatment apparatus comprising: a pressure treatment receiver vesselfor sterilizing particulate matter; an intensifier coupled to thereceiver vessel for increasing the pressure on the particulatecomponent; a recoverer for collecting the treated particulate matter;and a blender for blending the treated particulate matter with thetreated liquid matter.
 20. The apparatus as in claim 19 , wherein thereare at least two pressure treatment receiver vessels for sterilizing theparticulate component, the vessels connected to the liquid component andparticulate component separator.